Document a3YqKMjQ0Xp25xmGEKRorRbN

' >,f/'A s i Status Report SUSPENSION POLYMERIZATION OF VINYL CHLORIDE: UTILIZATION OF TECHNOLOGY OF PROCESS 5 AND PROCESS 6 R. C. Wise J. C. Alexander W. H. Nelson J. F. Erdmann, Group Leader DATE i April 28, 1960 FILE NO; B; 20:220-32 Project No: 510C SUMMARY Experimental polymerizations have been conducted in both production and pilot scale equipment to adapt Process 5 and Process 6 to the Suspension Vinyl Resins Unit at Location 514. Under the guidance of Dr. Hans Bauer of Burghausen, Germany, conditions were established for fullscale operation of these two processes, although only Process 5 is presently capable of producing salable resin. ~ Process 5, which utilizes Methocel 10 as the suspending agent and sodium bicarbonate as a buffer, produced resin of excellent initial color, as measured by the ICMT mill test. Physical properties of QXSH-5 and QXSJ-5 resins were near enough to the target properties to permit recommendation of immediate commercialization of both, and single experim nts with QXSA-5 and QXSC-5 resins demonstrated that the capabilities of Process 5 extend to those resins as well. Process 6 uses a poly(vinyl alcohol), Polyvlol VZ 200, as the suspending agent, Mersolat sodium alkyl sulfonate as a surfactant, calcium chloride as a surfactant modifier, and calcium carbonate as a buffer. Experimental Process 6 resins possessed relativ ly poor initial color, and although the color can be improved by addition of lauric acid to the polymerization charge, these resins cannot be- recommended at this time for commercial production. Process 5 could not be operated successfully in the autoclaves equipped with the Mixco turbine agitation systems, and a complete changeover to Pfaudler-type agitation is ther fore necessary for commercialization. Process 6, on th other hand, can be operated with either the Mixco or the Pfaudler system. However, a considerable part of the technology of Processes 5 and 6 is concerned, not with agitation or recipe, DEVELOPMENT DEPARTMENT Union Cahmoc Chemical* Company OUT* CHARLESTON, WEST VIRGINIA ucc 041 ms * B:20:220-32 2 but with the need for precise, reliable methods of charging and operating the autoclaves if resins of consistently high quality are to be produced. Recommendations in this ar a include the use of simpler methods of control, arrangement for prompt analyses and evaluations, establishment of fixed responsibility for the various steps in the polymerization procedure, and general modernization and simplification of the production equipment. These two processes establish new areas for investi gation, and extensive developmental effort is planned to adapt the processes to the various types of resin currently being produced. In addition, experimental determination of th full significance of the several process variables must be undertak n to obtain greater insight into the technology behind th new processes. INTRODUCTION For some time the poly(vinyl chloride) r sins produced in the Suspension Vinyl Resins Unit,at Location 514 have possessed significant shortcomings, particularly with regard to initial color of plasticized formulations. In addition the manufacture of poly(vinyl chloride) by suspension polymerization has not undergone sufficient technological advance to permit a worthwhile profit under current market conditions. Therefore when samples of poly(vinyl chloride) resin manufactured in Germany by Vacker-Chemie exhibit d excellent initial color, equivalent or superior to that of most domestic competitive resins, arrangements were made wh r by information regarding the German production would be made avail able to interested persons in South Charleston. Accordingly, a project team representing the Development, Production, and Engineering Departments visited the Vacker-Chemie plant at Burghausen to determine whether Vacker technology could be applied toward solution of the local problems concerning resin quality and operating efficiency. The information obtained in Germany (1) indicat d that without any exotic methods, materials, or equipment, Vacker-Chemie was able to produce resins of consistently high quality. In particular, two types of resin were consider d more readily adaptable than others for domestic manufactur . One of these resins, type HH 100/f, is produced with methyl cellulose as the suspending agent and with sodium bicarbonate as a buffer salt. It has excellent initial color, low fisheye content, good plasticizer absorption, and excellent el ctrical ucc 041019 B:20:220-32 3 properties. The other resin, type H 100, is produced with poly(vinyl alcohol) as the suspending agent, and with an anionic detergent and several salts added. Ibis resin features excellent hot-processing characteristics and extremely low fisheye content, but is inferior to type HH 100/f in color and electrical properties. The decision was made to operate these two Vack r processes in the suspension polymerization equipment at Location 514, and efforts along this line were begun on production and pilot scale as soon as the tour party return d to this country. Hbwfcver, to assist in expeditious adaptation of the Vacker technology to local facilities, Dr. Hans Bau r of the Burghausen plant was invited to South Charleston. Under Dr. Bauer's guidance, adjustments in recipes and operating conditions were made as required to achieve satisfactory properties in the resulting resin. At the conclusion of his visit Dr. Bauer recommended areas for continuation of the program (2). Those aspects of his.recommendations pertinent to production equipment were explored immediately upon his departure. Ibis report is intended to provide an account of the adaptation of Vacker technology to local equipment and procedural capabilities. To ensure complete understanding, the resins produced under the Vacker Influence will be differentiated from regular production runs by addition of "-5" or "-6" to the customary four-letter code designation (3). Specifically, the process for production of HH 100/f resins is Process 5, and that for H 100 resins is Procsss 6. Ref r nee to any or all procedures and recipes which arise from information from Vacker-Chemie will be accomplished in this and all futur reports by use of these new terms. An equally important reason for this designation is to eliminate the possibility of associating future commercial resins with their German origin through accidental references. DISCUHSlOlt Tot investigation of the applicability of Proc ss and Process 6 technology to the equipment and organization at Location 514, three production autoclaves were made available for experimentation. Careful control of th production runs was exercised by assignment of technical personnel as monitors for each shift. Hie first series of experimental polymerizations began as soon as necessary equipment modifications were completed, and continued after 5 ucc 041020 B:20:220-32 4 Dr. Bauer's arrival, while he familiarized himself with the Mixco agitation system and with the Suspension Vinyl Resins Unit in general. Operating conditions for this group of experiments, which are presented in Table I, were based on production of Process 5 resin for two reasons. First, that process is inherently the simpler of the two under consid ration; and second, all necessary raw materials were availabl by the time the production autoclaves were ready to use. The remaining production-scale experiments included in this report were conducted under the guidance of Dr. Bauer. Vhile Dr. Bau r was here, pilot-scale operations were made according to his suggestions; other experiments were conducted before and aft r his visit. I. Process 5 Resins The first attempts at production of Process 5 resin (Table 1) were performed without alteration of the production equipment except for that associated with resin recovery. Agitation was accomplished by use of three 31.8-inch, 7-bladed~ Mixco impellers, those in use for normal production of suspension poly(vinyl chloride). Conditions for production of QYSM-typ resin were chosen to permit ready comparison of the Process 6 resins with standard production resins and at the same time to eliminate the need for use of a molecular-weight degrader which might have Influenced the results to an indeterminate ext nt. The nominal recipe for Process 5 includes Methocel 10 as the suspending agent and sodium bicarbonate as a buffer salt. The operating conditions utilized as the process was developed locally are listed in Table IX. Hie particle size of the resins produced with a nominal Process 5 recipe was considerably larger than expected, and the fisheye content was excessive (Experiments 1W through 8T, Table 1111. By variation of agitator speeds and suspendingagent concentrations the particle size was reduced to desirable levels, but the fisheye content remained intplerably high in all instances. Dr. Bauer explained the deviation from desir d performance in terms of the quality of the agitation. In order to prevent the formation of hard resin particles it is necessary to provide high-speed, low-shear flow in the auto clave. the Mixco agitation system installed in the production autoclaves provides maximum shear with a relatively low amount of flow. ucc 041Q2) B: 20:220-32 5 The validity of this explanation was tested by removing three of the four side-mounted baffles from one of the autoclaves and replacing the Mixco turbine impellers with a single 51-inch impeller with three straight, glass-coated blades. The advantageous effect of this alteration was clearly apparent (Experiments 5W and 11W, Table III). Th median particle size of the resin was reduced from 280 to 105 microns, and the flsheye rating decreased from 200 to 20 p r square foot on 17.5-mil film. The operating conditions wer essentially identical for these two runs, with the exception of the type and speed of agitation. Vith the Mixco agitation system the maximum speed attainable within the power limitations of the drive motor was 110 rpm, whereas the Pfaudler-typ impeller could be run at 125 rpm, the maximum drive spe d, with only some two-thirds of the available power being consumed. Thus Process 5 was adapted to local equipment with only this relatively inexpensive alteration in the agitation. In all likelihood the final arrangement for full-scale manufacture of this resin will present fhrthpr benefits, if care is taken to design the optimum impeller-baffle combination for th existing autoclaves. II. Process 6 Resins Operation of Process 6 was expected to be more nearly like standard local production than Process 5 had been. Process 6 recipes utilize a combination of poly(vinyl alcohol) suspending agent and an anionic surfactant, and in this r spect are not unlike the recipes often used in local production of certain resins. In the nominal Process 6 recipes, Polyviol VZ 200 was the specified poly(vinyl alcohol), and Mersolat sodium alkyl sulfonate was the surfactant. To these basic ingredients calcium chloride was added as a surfactant modifier, and calcium carbonate, as a buffer. The operating conditions of the experiments performed with the Process 6 recipe are listed in Table IV, and the evaluations of the resulting resins arm presented in Table V. In production autoclaves agitated with Mixco turbine impellers,the Process 6 recipe, unlike the Process 5 recipe, produced resin of a fine particle size and a low flsheye rating. The particle sizes, in fact, were somewhat smaller than desir d, in that about 30 per cent of the resin passed through 270-mesh screen. Such a resin would probably be unsuitable for several types of processing, notably dry-blending operations. However, ucc 041022 B: 20:220-32 6 Dr. Bauer had no doubt that the particle size could b incr as d by suitable adjustment of agitator speed, concentrations of recipe ingredients, and saponification number of the poly(vinyl alcohol) selected as the suspending agent. The principal deficiency in the Process 6 r sins as produced in this series was in initial color (Table V). Dr. Bauer had never observed in this type of resin the yellow cast which overcame the plasticized resin on the mill. He suspected that impurities in the calcium chloride or the calcium carbonate might have been responsible for the poor color. Accordingly, the reagent-grade materials were subjected to semiquantitativ analysis by the flame spectrometer, along with samples of the corresponding materials used by Dr. Bauer. Hie results of this analysis, which are presented as Appendix A, provide no corro boration of Dr. Bauer's suspicions. Whatever its source, the poor color can be Improved markedly by addition of lauric acid to the autoclave charge The effect of such an addition was demonstrated in th 10-gallon E8 autoclave (Experiments 718 and 720, Table VIII). The only difference between the operating conditions of these two runs was the presence of lauric acid in Experiment 720. Initial color as measured by the ICHT test was improved from a r flectance of 78 to 112. Although experiments in E8 and other autoclav s of similar size have often produced erratic results in the past, the combined evidence of these runs and Dr. Bauer's statements establishes the use of lauric acid in the Process 6 recipe as a practical method of achieving the desired initial color in the Process 6 resin. III. Process 5 and Process 6 on Pilot Scale To provide a guide for initial operations in production equipment, several polymerizations were conducted in pilotscale autoclaves. The conditions employed in these polymeri zations are listed in Table VI and Table VII, and the evaluation data for the resulting resin are located in Table VIII. With the Process 3 recipe (Table III), QXSM-5 resin was produced in the 10-gallon, stainless steel E8 autoclave, equipped with 7-lnch Mixco impellers. Several different charging and operating procedures were used, but in nearly every instanc the particle size of the resulting resin was very large, and the fisheye content was excessive (Table VIII). However, the ucc 041023 B:20:220-S2 7 initial color of the Process 5 resins produced in E8 autoclave was considerably improved over that encountered in ordinary runs. The average value of the ICUT tests on these resins was approximately 110, whereas a typical resin from previous work would be expected to yield a value of approximately 65. As in production equipment, the Process 6 recipe proved more appropriate for the Mixco agitation system than had the Process 5 recipe. The Process 6 resin was finer (average median particle size about 235 microns), and the fishey content was about 30 per square foot on 17.5-mil film. The initial color was not satisfactory for the nominal Process 6 recipe, but upon addition of lauric acid, as mentioned previously, the performance of the resin in that respect was improved' signifi cantly. Polymerizations by Process 5 were performed also in the 500-gallon, glass-lined E16 autoclave equipped with Pfaudler-type agitation. These runs are included in Table-III, and the evaluations of the resulting resin are in Table VIII. However, numerous operating difficulties were encountered in E16 autoclave which rendered the results virtually useless. In any event, neither corroborative nor contradictory evid nc was obtained in the short period of E16 operation. IV. Resin Recovery From each experiment of this series two resin samples were evaluated. One was the flash-dried resin, and the other was resin drained from the autoclave and dried in the Proctor and Schwarlz tray dryer. In practically every run, the r sin from the tray dryer possessed significantly superior initial color, compared with the resin from the flash dryer. This relationship has been observed invariably over a long period of time, but has always been challenged on the ground that either the wet-stripping tank or the flash dryer could hav produced the ill effect. The elimination of the Wet-stripping tank from these runs, accomplished for just this reason, leaves no reasonable doubt that the flash-drying system of th Suspension Vinyl Resins Unit does considerable harm to the resin. ucc 041024 B;20:220-S2 8 V. Status of the Program with Regard to Specific Resins The program for utilization of Process 5 and Proc ss 6 technology embraces two distinct areas. One is the development of techniques and recipes to permit optimum operation of production equipment in these processes and to develop the best resins of which the processes are capable. The other area is the application of these techniques and recipes to specific types of resin already being produced in the Susp nsion Vinyl Resins Unit. To demonstrate the applicability of Process 5 and Process 6 to current resin production, Tabl s IX, X, XI, and XII present a comparison of several important properties of each with designated target properties (4). The examples in these tables are specific runs whose results ar considered representative. A. QXSM QXSM-5 resin, the Process 5 counterpart of QYSlf ' resin, exhibited significant improvements over standard pro duction resin (Table IX), particularly in initial color of plasticized formulations and in fisheye content. In comparison with the target, which represents the properties a resin must have to be generally competitive in the current market, QXSM-5 resin is somewhat low both in specific viscosity and in apparent density. The low specific viscosity should not be considered an actual deficiency, since it can be altered readily by simple adjustment of the concentration of molecular-weight degrader in the charge or by small changes in the polymerization temperature. Some development work will be required to lncreas the apparent density without incurring the generally attendant reduction in absorption. However, the magnitude of this adjustment, from 28 to 32 pounds per cubic foot, is small enough that no great difficulty is foreseen, and in th mean time, the QXSB-5 resin now available should satisfy all but a fe of the potential users. QXSM-0 resin, it can be seen, deviates considerably from the target, principally in possessing too fine a particle size and In exhibiting poor initial color. The high incidence of hard resin particles should not be a significant probl m. Process 6 is designed to produce practically no fishey s, and the occurrence of fisheyes in the experimental resins is considered a result of experimental inadequacies. However, the other discrepancies will probably require considerable effort to attain acceptability. ucc 041025 B:20:220-S2 9 B. QXSJ QXSJ-5 resin, as produced in the period cover d by this report, falls very little short of complete attainm nt of the target properties (Table X). In fact, insofar as th target properties accurately describe the actual requir m nts for the resin, QXSJ-5 resin must be considered ready for immediate commercialization. Hie properties of QXSJ-6 resin differ significantly from QXSJ-5 resin only in lover absorption and smaller particl size. However, since Increasing the particle size oft n involves a reduction in absorption, the readiness of QXSJ-6 for commercial application cannot be assumed. C. QXSA and QXSC The need for processes for manufacture of QYSA and QYSC resins was not so urgent as that for QYSM and QYSJ resin, and therefore experimentation with each was limited to one run at the end of the series. However, in both instances th resin produced under Process 5 conditions possessed properties quite close to those designated as the target (Tables XI and XII). It is apparent that the capabilities of Process 5 xtend to both QYSA and QYSC resin, although the exact status in th se areas cannot be estimated accurately. Y. Operating Conditions The nominal recipes for Process 5 and Process 6 were presented in an earlier report (1), and the recommended range of permissible variation in the concentration of each of the ingredients was listed also. No need for modification of the previously reported limits has become apparent in th studies to date. However, as further efforts are made to provide a complete line of resins with the desirable charact ristl<jft>*i th* new processes, departure from these nominal condition* is inevitable. The following discussion of the signifies*** of the several process variables should provide a basis for orderly progress into those areas which future needs will prescribe. uCC 041026 B: 20:220-82 10 A. Recipe According to Dr. Bauer, the two recipes which constitute Process 5 and Process 6 may be used interchang ably for production of a given type of resin. That Is, a satis factory resin may be made with either process. Hbwever, Process 5 produces a resin of superior color and electrical properties, whereas Process 6 yields a resin of relatively easy processing behavior and with virtually no fishey s. When these slight differences cover properties of great importanc to a particular customer, then the preference for one process over the other becomes significant. In other circumstances the only factor available for making a choice is the relative ease of operation and adaptability to existing equipment. Process 5, by virtue of its fewer components, is inher ntly easier to operate. Process 6, on the other hand, has proved more readily adaptable to equipment and procedures in use for standard production. B. Suspending Agents Of great significance in the technology of Process 5 and 6 is the strong emphasis which is placed on the suspending agent. The exact relationships between physical properti s of the suspending agent and characteristics of the resulting resin are not available, and will not be until considerable, small-scale, experimental effort has been devoted to that problem. However, regardless of the type of suspending agent, several generalizations will apply. First, the suspending agent must be completely and uniformly dispersed in the autoclave. The only way to ensur this condition is to prepare the charge solution of susp nding agent in water in such a way that guarantees the compl te absence of gels and undissolved particles. Any of several methods nay be employed to achieve this objective, but what ever the means, efficient production of quality resin demands a virtually perfect solution of suspending agent. Another consideration is the accuracy of charging the suspending agent solution to the autoclave. Although th relatively low precision of this experimental series, which resulted from the many changes in operating conditions, did not permit definitive demonstration of this effect, Dr. Bauer ucc 041027 1 B:20:220-32 11 - was quite specific in stating that very small errors in charging the suspending agent can cause significant variations in th characteristics of the resin produced. To satisfy this requirement for accurate charging will necessitate the pro vision of accurate weighing or metering devices and th implementation of a firm schedule for determining the solids content of the solution. C. Additives The recipe for Process 5 includes a buffer salt, sodium bicarbonate. Although there is nothing to indicat that sodium bicarbonate exclusively is required, Process 5 t chnology teaches that some buffer is necessary for consistent polymeri zation results. In operations of Process 6 several polymerization additives are required. Mersolat, a sodium alkyl sulfonate detergent made in Germany, is included for its effect on particle characteristics. In this recipe calcium chloride~isadded as a modifier of the surfactant, and calcium carbonat is added as a buffer, again to improve reproducibility of results. The basis for the choice of these particular ingredients has not yet been determined, but no doubt exists that th se or equivalent additives are necessary for desirable results. Vorthy of particular notice in the case of Process 6 is the fact that previous local recipes, which utilized a different grade of poly(vlnyl alcohol) and another surfactant, w re in capable of producing resin with the required initial color and low fisheye content. Thus, until more specific information can be obtained, these original Process 6 ingredients must b considered an essential part of the process, even though their eventual replacement by domestic materials is quite desirable. D. Other Polymerization Variables Process 5 and Process 6 Involve no new consid rations with regard to the remaining polymerization variables. The molecular weight of the produced resin is determined by the polymerization temperature or may be modified by use of a degrader, such as trichloroethylene. Dilauroyl peroxide, regularly used locally as the polymerization initiator, is utilized in Process 5 and Process 6 as well. High standards of purity are demanded for monomeric vinyl chloride in both the new and the old processes, and the need for water free of dissolved salts and inert gases likewise is recognlz d in both. ucc 041028 B:20:220-82 12 E. Operating Techniques Recipes and polymerization conditions constitut only a part of the technology on which Process 5 and Process 6 are based. Of perhaps equal importance is the concept of more careful operation throughout all phases of production. At every stage in the investigations into these new processes, from the initial inspection of Process 5 and 6 production facilities to the adaptation of the processes to local equipment, certain considerations were continually.demonstrated as vital to successful operation. Cleanliness over the entire commercial operation is a prime requisite for achievement of good results. Resin remaining in the autoclave from previous runs leads almost invariably to the formation of fisheyes by providing a hard particle on which excessive agglomeration can occur. In addition, particles exposed to several polymerization cycles are likely to exhibit greatly inferior color by virtue f repeated exposure to unnecessary heat. Any particles of dirt allowed to enter the autoclave in the water or monomer will produce similarly undesirable results; and, if the dirt should contain iron salts, for example, the adverse effect on initial color and thermal stability would be sufficient to overcom any advantage gained by improvements in the recipe or the proc ss. Accuracy in operation likewise has been shown essential to successful production. Previously successful commercial ization of the principles of Process 5 and Process 6 has involved careful metering of all components of the autoclave charge, whereas local procedures have been accurate only when conditions were ideal. For example, in normal production the charge of water to the autoclave containing all the other charge ingredients has been measured by a probe in the sight glass of the autoclave. If there is any appreciable amount of foaming or if the sight glass is in any way occluded, two conditions which occur-often and without available remedy, the amount of water actually charged can quite conceivably vary considerably from run to run. The quality of resin will vary with the charge, and hence reproducibility will be poor. Reversal of the order of charging so that the monomer is charged last can lead to even gr at r ucc 041029 1 B:20:220-S2 13 - chance of error. Accuracy of charging other ingredients of th recipe, while not so obviously inadequate, is in many instances suspect because of an absence of specific controls and checks, which in turn is due in large measure to a lack of fix d responsibility for the numerous steps in preparing and charging the polymerization ingredients. In short, the secondary aspect of the new technology is care, some of which can be built into the operating procedures by provision of accurate, convenient, and simple measuring devices, and some of which can arise only from increased attention by operating personnel to specifically assigned, carefully detailed procedures. When such reliability has been achieved, still another need remains. The often-fickle nature of polymerizations and the impossibility of perfect performance by operating personn 1 and equipment will always result in some poor runs. It is necessary that one poor run not be permitted to destroy th _ value of other, more satisfactory runs. The only way to guard against such an occurrence is to evaluate the resin for each run before it is included in a blend. The use of a common blow down tank for the resin from several runs, as normal operating procedures require, makes timely evaluation impossible and may cause one poor run to spoil three or four times its own amount of resin. Tests must be devised and implemented to permit shift-by-shift, run-by-run evaluation of the resin. In instances where Process 5 and Process 6 have achieved commercial success, this has been done. EQUIPMENT For the full-scale polymerizations which are dis cussed in this report, three production autoclaves (CIS, C16, and C17 at Building 176, location 514) were us d. Each of these stainless steel autoclaves has a capacity of 4600 gallons. At the start of this series each autoclave was equipfite with stainless steel Mlxco Impellers mounted on a vertical shaft, which was supported at the top of the autoclav by a mechanical seal and thrust bearing and at the bottom by a steady bearing. Agitation changes, which have already b en discussed, involved only the replacement of the turbin impellers by a single, glass-coated, straight-vane impell r located near the bottom of the autoclave. Each autoclave was equipped originally with four side-mounted baffles; with the altered agitation three of these baffles were removed. ucc 041030 B: 20:220-32 14 Alteration of the existing recovery system was required because, unlike in normal production, resin from each run had to be processed separately and because the experimental processes called for washing the resin before it was dried. The blowdown tank was therefore bypassed, and a "skin trap" was installed to remove any large aggregates of resin. The wet-stripping tank was used as a wash tank, but no st am was fed to it; the Bird centrifuge and the flash dryer were used without physical alteration. The path of the resin thus was from the autoclave through the skin trap into the wet-stripping (wash) tank, then to the Bird centrifuge and on into the flash dryer. OPERATING PROCEDURE In many respects the operating proc dur s used in this series were the sam as those used for regular production. However, some of the proc dur s were sufficiently different to warrant special mention. I. Process 5 Water at 50C was first charged to the autoclave to a level measured by insertion of a rod of a specified length. The suspending agent, Methocel 10, was dissolved in water in a 50-gallon stainless steel drum (it was first slurri d in 80"C water, then agitated in cold water until completely dissolved) and then pumped through a Ful-Flo filter into the autoclave. Sodium bicarbonate powder was then poured into the autoclave, followed by the dilauroyl peroxide catalyst. The autoclave vapor space was then evacuated for a half hour at a t mperature of 50C and a pressure of 2.2 psia, with the agitator turning slowly to aid diffusion of dissolved gases from the wat r. At the end of the evacuation a small amount of vinyl chloride was added to break the vacuum, and the autoclave was cool d to 30*C. The vinyl chloride charge was added at the lower temperature so that the autoclave pressure would not xc ed that of the vinyl chloride supply line. Any required trichloro ethylene was also added at that time. With the charg completed the agitator speed was increased to the specified level, and the autoclave was heated to operating temperature. uco 041031 B;20:220-S2 15 - Polymerization was conducted until the specified termination point was reached, at which time the unreacted monomer was stripped from the autoclave while operating temperature was maintained. Stripping in the autoclave was made practical by the high degree of conversion (greater than 90 per cent) to which these polymerizations could be carried while preserving the desirable resin properties. The stripped charge was next cooled to 30C and fed to the recovery system by application of nitrogen pressure to the autoclave. The slurry, which contained about 30 per cent total solids, passed first through the skin trap for removal of any large aggregates of resin, and then into the wash tank, where water was added until the total solids content was about 10 per cent. A liquidlevel instrument on the wash tank actuated a motor valve which regulated the flow of slurry into the tank. From the wash tank the slurry passed into the Bird centrifuge, where as much wash water was added as was possible without incurring resin- loss s in the effluent liquid. The resin then entered the flash dryer, and when dry it was directed into a clean storage bin. II. Process 6 Procedures for Process 6 were essentially the same as for Process 5, with the obvious exception of the charg . Th suspending agent, Polyviol VZ 200, was first slurried in cool water and then dissolved in hot water prior to being pumped through a filter into the autoclave. Next the wetting agent, Hersolat, was dissolved in water and pumped into the autoclave. Calcium chloride was also predissolved before being pumped into the autoclave; calcium carbonate was added next, followed by the dilauroyl peroxide initiator. Ftom this point on, th remaining procedures of Process 5 were followed exactly. RESIN EVALUATION During all steps of operation, samples w re taken to permit evaluation of all phases of the experimental series. A list of the samples and the tests performed on each sample is presented as Appendix B. One of the most critical tests to which the r sins were subjected is the "ICMT"* te^t, which was develop d for evaluation of resins scheduled for use by Elm Coated Fabrics, Inc. The details of this test are available (5), and for the purpos s of this report complete description is unnecessary. For the ICMT test the resin is first compounded and then worked on a ICMT - initial color mill test ucc 041032 1 i B:20:220-S2 16 two-roll mill for a total of ten minutes. A numerical value for initial color is obtained by measuring the reflectance of specimens taken from the mill at 5 minutes and 10 minutes milling time. The sum of the reflectances of the two specimens is the number which represents initial color, with a value greater than 100 denoting satisfactory performance. The test listed frequently in Appendix B for aqueous surface tension refers, in addition to the standard det rmination by the Instron Tester, to a simplified method of determination which was received as a part of Process 5 and 6 control procedure. It consists merely of filling a specially designed pipet with the solution being tested and then observing the number of drops formed as the solution flows out of the pipet. Since both the concentration and th quality of the polymerization ingredients have an effect on the results of this test, it provides a simple check on the accuracy of charging the water-soluble components. The wet-milling evaluation was an innovation utillz d in this series. The test produced no new information, but it had the advantage of permitting evaluation of the resin immediately upon termination of the polymerization, before the resin was dried. Although the test itself is of little cons quence, such a method would be of great value in decreasing the likelihood of one bad batch of resin being permitted to enter and contaminate an otherwise satisfactory blend. The Development Department now has work underway to modify existing test procedures to permit such wet-milling evaluations. New procedures will probably be available for use by the time th production facilities have been modified to provide temporary storage space for rejected resin. The remaining evaluation procedures were standard tests, which have been performed and reported many times in the past. The results of all the tests have been evaluated, in order to obtain insight into the relationships between all measurable variables and the properties of the resultant resin. However, only those tests which were demonstrably significant are included in Tables III, V, and VIII. ucc 041Q33 B:20:220-S2 17 CONCLUSIONS The experiments included in this report constitute a significant forward step in the developm nt of high-quality, salable polyCvinyl chloride) resins. It is clear that future work in this area will refer back to this series as a plateau of understanding on which much, or p rhaps all, additional effort will be based. This establishment of a base for future work is the most important conclusion which can be drawn from this series of runs. However, ther ar also several features of the study which permit more specific conclusions. I. By use of Process 5 recipes and techniques, resins with exceptional initial color and with very low fisheye content can be produced immediately. Hie recipes are slmpl to employ,and the techniques are not difficult. But Proc ss 5 cannot be operated with the Mixco turbine impellers. Changing to a Pfaudler agitation system, or its equivalent, is an absolute requisite for utilization of Proc ss 5 on production scale. II. Process 6 can be employed in present autoclaves with current agitation systems, but the resin cannot be expect d to have the same excellent initial color as was achi ved in Process.5. It is likely that the color of Proc ss 6 resins can be improved to an acceptable level by suitabl changes in recipe and in polymerization conditions; and if this can be done, the virtual freedom from fisheyes of the Process 6 resins will be of great value. III. The adaptability of Process 5 resins to immediate production of current grades of resin has been demonstrated adequat ly. To the extent that local tests and specifications are true representations of resin requirements, the conclusion can be drawn that QXSJ-5 and QXSH-5 are suitable replacements for their counterparts in present production. How v r, it must be recognized that the ultimate test of any resin is satisfactory performance for the customer, and th refor final Judgment of Process 5 resins must await compl tion of customer evaluations, such as those already in progr ss at Blm Coated Fabrics, Inc. Ucc 047034 7 i B:20;220-S2 18 - IV. The acquisition of Process 5 and Process 6 places the Company in a position to compete for practically all the major resin accounts in the suspension poly(vinyl chloride) field. The capability is now in hand for production of resin with initial color at the very least equal to competitive resins such as Presto, Marvinol, and Escambia 2185. The only level not yet attained is that filled by Escambia 3185 resin in the premium-quality, "Crystallite" area. This is not to say that Process 5 resins will now overwhelm the market. The particle properties which determine preblend characteristics, ease of extrusion, and the like are not yet wholly satisfactory, and still other deficiencies may emerge when customer demands are heard. But with initial color and flsheye content under control, accomplishing the relatively slight improvements still required in particle characteristics should not present any great difficulties. V. The optimistic tone of these conclusions is based on reliable results; however, one major condition must be attached to any such predictions. Process 5 is capabl of producing these excellent results only if it is properly employed. The Suspension Vinyl Resins Uhit at Location 514 is not fit for production of Process 5 resins in its present form. The unit must be altered in accordance with forthcoming recommendations if the full benefit of Process 5 is to be enjoyed. RECOMMENDATIONS Because of the abrupt shift in thought effected by the emergence of Process 5 technology, specific directions of future effort should be laid out at this point in order to control any tendency toward overzealous utilization of the new information. The following recommendations are therefore presented, along with a strong urging, that they be analyzed most carefully before any altenastlve* are adopted. ucc 041035 B:20:220-32 19 I. Production Department A. Pfaudler-type agitation should be installed in all production autoclaves as soon as possible. No Process 5 runs should be attempted with the Mixco agitation system. B. Operational changes in Process 5 conditions should be confined within the range of conditions which have already been explored. Specified limits in recipes and in operating conditions, based in large measure on Dr. Bauer's suggestions, are listed in a previous report (2). C. A long-range program should be begun immediately for the orderly renovation of the Suspension Vinyl Resins Obit. First, the charging system should be simplified as much as possible to reduce the number of possible sources of contami nation and to provide maximum ease of accurate charging and operating. Second, the drying system must be overhauled and modified to ensure that resin hold-up or recycle is eliminet d. If reasonable efforts cannot effect this improvement, th n the drying system should be replaced completely. Even the very finest process control cannot overcome the damaging effects of an inadequate recovery system. D. Steps must be taken to impress upon operating personnel the absolute necessity for faithful, unvarying adherence to the newly established operating procedures. The sensitivity of Process 5, and Process 6 as well, to relatively small changes in process conditions demands the very greatest care of operation, without which the major advantages of the new technology will be lost. II. Development Department A. Pilot-scale experiments will be undertak n for the development of a firmer understanding of the principles behin#>firoGess 9 and Process 6. Modifications of the nominal reeipsPV including experimentation with alternative materials for use as suspending agents, surfactants, and other additives, will be investigated. The 10-gallon and 15-gallon autoclaves are satisfactory generally for primary experiments with novel operating conditions. ucc 041036 B:20:220-82 20 - B. For reliable, reproducible engineering data, larger pilot-scale autoclaves must be made available. The ideal size probably lies between 30 and 50 gallons. Autoclav s larger than this would produce good results, but the cost of operation would be unnecessarily high. It is therefore our intention that an autoclave in the size range of 30 to 50 gallons be obtained and that this autoclave be used as the sit for basic work on the variations in particle characteristics which will be necessary as the area of application of Process 5 and Process 6 resins becomes broader. C. Intermediate-scale polymerizations will be undertaken in the available 500- and 600-gallon autoclaves to pursue the leads offered by the smaller equipment. In addition, attempts will be made to establish scale-up factors t permit accurate correlation between development and production operation. ACKNOWLEDGMENTS In the operations described in this r port the cooperation and assistance of the f llowing persons are gratefully acknowledged. I. The Suspension Resins Department under J. C. McIntosh of the Production Department provided the equipment and personnel for the polymerizations. II. Personnel of R. G. Massey's group of the Development Department were responsible for operating pilot-scale auto claves and for tray-drying the numerous slurry samples from the production runs. III. P. T. McCoy, of J. J. Brezinski's group of the Dev lopment Department, developed and conducted the novel testing procedures introduced in this series. IV. ^Parsonnel of the Quality Control laboratory, under the dlrectioc of J. W. Chat fie Id and C. J. Haines, exp nded considerable effort to provide the evaluation results as rapidly as possible, thereby reducing delays between runs in the series. ucc 041037 1 B:20:220-32 21 - V. Dr. Hans Bauer, besides providing the polymerization recipes and the technology for the most profitable adaptation to local equipment, contributed greatly to the present m asure of success by his never-ending insistence on attention to minute details. In addition, much of the comment of this report is based on his explanations, stat d or implied, of the relative importance of the several aspects of the study. BIBLIOGRAPHY (1) Erdmann, J. F., et al., Polyvinyl Chloride Suspension Resins: The Wacker-Chemle Process: Report of Plant Visit. November, 1959^ January 22, I960. (2) Erdmann, J. F., Suspension Poly(Vinyl Chloride) Resins by Tacker-Chemle Processes! Project Review, January 29,. i960, Development Department, February 24, I960 IB:20:220-mV). (3) Hanks, G. J., Jr., " Suspens ion-5 " Res ins, Memorandum to Vlnylite Area Supervisors and Department Heads, February 22, 1960. (4) Engle, D. L., Suspension Resins Manufacturing Targets, letter to M. E. Sutherland, February 9,i960 IB:20:500). (5) McCoy, P. T., Unpublished material, laboratory Notebook D-3346. LABORATORY ACCOUNT: 2612 PERIOD: December 1, 1959 to February 15, 1960 Attachment*: << ^SKStixes nwh ucc 041038 B: 20:220-32 - 22 - TABLE I SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Operating Conditions for Initial Experimentation with Process 5 in Production Autoclav s Autoclaves: Agitation: Constant operating condition^'; Type of resin produced: 4600-gallon, stainless steel with falling-film brine jacket Three 31.8-inch, 7-bladed Mixco impellers and 4 side-mounted baffl s Autoclave charge level, 90 per cent; polymerization temperatur , 57C; concentration of dilauroyl peroxide catalyst, 0.088 per cent of VC1 QISH-5 Expt Autoclave No. No. Monomerto-Vater Ratio Oononntrations, per cent of VC1 Sodium Methocel 10 Bicarbonate Agitator Speed, rpm Operating Pressure, psig Reaction Time, hr T rmination Point IV C15 2V C15 31 C15 5V C15 61 C15 71 C15 8V C16 37/63 30/70 30/70 37/63 37/63 37/63 37/63 0.09 0.09 0.068 0.09 0.13 0.18 0.15 0.11 0.11 0.083 0.11 0.127 0.127 0.153 84 84 84/110 110 110 110 110 124 127 126 124 127 130 132 13.0 12.2 13.25 11.5 12.25 10.75 10.5 Pressure drop Pressure drop Pressure drop Pr ssure drop Pressure drop Pressure drop Tim OCOJ B: 30:230-83 i - 33 - TABU II OOBBUSICIf POLYVXRIZATIOM OF VIOTL CHLORIDE Conditions for hperlmentatlon eltb Process 5 Id Production Autoclavas IiiImIith: Agitation: Constant operating conditions: IRQ# n\Taa, stainless atsal vl tb la1ling-film brine Jacket Qas IpilsQk, etra1ght-bleded, gleea-llned Pfaudlar-tjrpe agitator and 1 side-aountsd be file As^>Bjfy<6|ir|e leael, 33 par cent; monoMr-to-eatar ratio, 37/63 Sapt So. * n 16V 16V 16V Autoclav So. CIS CIS CIS C16 CIS 13V 16V 17V 30V CIS C16 C17 C17 31V CIV 33V CIS CoKHtntlou. ptr cent of ICl ----in Boatii- 11 fc--< Diulilauroyl -- atbocel 10 Bicarbonate Paros Ida Trichloro ethylene 0.10 0.00 0.113 0.13 0.15 0.16 0.13 0.16 0.16 0.16 0.066 0.066 0.12 0.13 0.13 - 0.10 0.13 0.13 0.136 0.13 0.16 0.16 0.16 0.066 0.166 0.166 0.166 1.0 1.0 1.0 1.0 0.13 0.16 0.105 2.3 0.16 0.16 0.36 BolymerIsatIon Temperature,*C 57 57 57 S7 57 Agitator Speed, rpm 137 123 136 125 135 Operating Pressure, palg 138 127 135 134 134 Reaction Time, hr 10 10 10.3 10.6 11 Ten 1 nation Point Time Time 5 pel AP 5 psl AP 36 pal AP 57 136 130 13 AP 57 125 125 0.7 5 pal AP 67 136 127 8.6 5 pel AP 67 136 135 8.76 35 pal AP 57 135 134 8.5 5 pal AP SO 135 103 13.5 5 pal AP Type Real a Produced QXSb-5 QXSM-6 OXSH-8 QI8M-5 OUH-5 OPttJ-s qxsj-5 qpuj-s QUJ-5 088A-5 OPUC-6 041040 I Kxpt Ho. Baal nil Basin Type IV 31 3H SI 6V 7V V sv 11V 16V 16V 19V quB-s qun-6 qESM-5 qtsa-s QE8M-3 qksm-s n-s qXSM-3 qiSB-5 qUB-5 qum-B <***-* Specific Viscosity 0.175 0.177 0.176 0.163 0.161 0.163 0.163 0.175 0.173 0.175 0.177 0.176 24 TABU III SUSPENSION POLYMERIZATION OF VINYL CHLORIDE iMOloa r W . ' f ''I -1 .:r t Data for Process 3 Basins (See Tables I and Produced Eaperinentally In Production II for Operating Conditions) Autoclaves ft;:- - ` . ' : ^ / .r p. Appsaaot Density. -4| ib/o ti 1 '*r 25 " 46 ' 31 45 34 46 S3 62 26 54 29 49 29 55 30 50 26 40 26 54 26 49 27 47 Persorptlon, per cent 173 163 152 254 303 IBS 164 233 218 - 169 174 Particle Characteristics Through Median, 270-Mesh, microns Dispersion Skew per cent 300 330 300 260 235 110 120 160 105 170 115 90 -2 -1 -- -6 -2 - 13 - 14 63 +0.03 6 590 +0.40 75 -0.07 3 65 +0.13 10 35 0 15 Bard Reain Particles Per Square Foot on Mil Thickness 6 10 17.5 50 200 70 so 40 70 50 100 20 2 10 3 200 300 75 200 200 200 100 100 30 2 20 5 300 300 20 200 200 70 100 20 20 3 5 5 UI qxu-s 1SV qu-i-s 17V quj-s 90V QBSJ-S 0.142 0.145 0.143 0.147 29 31 20 31 50 50 47 42 156 190 150 145 115 -6 53 +0.00 6 70 -0.15 3 45 0 10 3 50 0 10 5 10 05 50 5 0 2 ICMT 111 That Color Press "C" Test 100 109+ 107 99+ 96+ 103+ 109 111 103+ 90+ 107+ 105+ 74 60 63 65 82+ 71 73 73 62 60+ 79+ 64+ 109+ 116 106+ 112 62 74+ 73+ 75 21V u-s 0.123 32 44 - 165 75 0 7 10 10 5 106 73 UI worn: oC O CD O 6C-B 0.217 30 51 - 5115 45 0 22 3 101+ 64 Color testa to bo ccaaparable aunt bs ssde on standard plaque thicknesses. The or - associated with boh reflectance values indicates a plaque slightly thlckar or thlsnar tbas jprescribed, Thun, a reflectance sith a + la as uacorracted reading which ia lover than the true value since the 9loans la tblcksr sad absorbs sorti llvbt. 9:30:330-83 - 36 TABU tV SU&PBHSIOII FQLWESIZATIOK OP VIKYL CHLORIDE Conditions for bperl*eBtatlon with Process 0 In Production Autoclave* Autoclave*: 4800-galloo, *talnl**a eteel with falling-til* brine Jacket Agitation: Three Sl.S-iocb, 7-blad*d Slxco lapellera and 4 alde-aounted baffle* Constant operating coadltlneg:' Antoclave charge level, BO per cant; *ono--r-to-eater ratio, 33/87; agitator speed, 110 rp* Sspt Mo. ion 13W 14W Autoclave no. CIS Cl? CIS POlyvlol VZ 300 0.33 0.31 0.33 Concentratlone . par cast of TCI Calclua GUClW Klauroyl Maraolat Chior Ida Carboaata Paroxlda o.oss 0.047 0.0004 0.070 0.003 0.047 0.0004 O.OSO O.STO 0.048 0.0000 0.000 Trichloro ethylene 0.1? 1.0 1.0 Polyaer lza tl on Ttaaperature, *C 3? 80 88 Operating Pressure, pels 130 133 134 Reaction Ti*e, br 14.33 14 14.33 Termination Point 85 paig SO pnlg SO pelg Type Resin Produced qxsn-s QX8J-6 4X8J-6 ucc 041042 T B:30:330-B3 - 36 TABU V 8DBPBK310N POtVMBHIIATlOB OT VIXY1. CHL0B1DB Bat* for Proc*a 6 Basina Produced experimentally In Production Autoclaves (Boo Table IV foT Operating Conditions) Kxpt Bo. 10V 13V 14V BoaInal Besln Type QUM-6 QEBA-6 OUJ-6 Specific Viscosity 0.173 0.130 0.140 Apparent Density, lb/cu ft 36 31 30 Absorption, per cant SO 35 45 Persorption, per cent 196 - - Median, eicrons 65 55 65 Dispersion Bfces Tbrougb 370-Nesb, per cent 38 31 30 Hard Besln Particles Per Square Foot on Xil 'Thickness 6 10 17.5 50 70 30 5 50 6 5 30 10 I CUT Hill Test 40+ 87+ 89 Press 1 Test 63- 73- 63- oon < L latoclm E8: latacltn El6 - 27 TABU VI SUSPENSION POLYNKBIZATION OF VINYL CHLOKIDE Operating Oaegltlona for bperiMntatlon with Process S in Developeent Autoclaves EB and E16 10-gallon, stainless steel aMk Olieulating-sater Jacket, agitated by tvo T-incb, 4-bladed Nlaco lspellers and fitted eitb 4 side-sounted baffles 500-gallon, glass-Heed ELwipwitiil-wter Jacket, agitated by one 36-inch, 3-bladed, glass-coated, sloped tape Her and fitted elth 1 suspended beffle "^T1 ' bpt No. CM 67 fiM 700 701 703 703 704 709 706 707 706 700 710 711 716 710 717 AutoeIsvs Mo. M SB SB SB SB SB 30 SB ES SB B SB SB SB SB SB SB to-Stsr Batlo 96/63 96/63 96/63 96/63 96/63 96/63 36/63 96/63 36/63 35/65 35/65 35/65 35/65 35/65 35/65 35/65 36/65 95/65 Methooel 10 o.om ur 0.0675 (1) 0.0675 (1) 0.0675 (1) 0.0675 0.0656 0.0656 0.0676 0.0676 (1) 0.0676 0.0675 0.0675 0.0675 0.0675 0.0675 0.0675 0.0675 0.0676 Bicarbonate 0.1135 0.1135 0.1135 0.0644 0.0644 0.1136 0.1135 0.1135 0.1135 0.1135 0.1135 0.1135 0.1135 0.1136 0.1135 0.1136 of VC1 Diiauroyi Peroxide 0.0635 0.0635 0.0635 0.150 0.0635 0.0635 0.0635 0.0635 0.150 0.150 0.150 0.150 0.150 0.150 0.150 0.150 0.160 0.150 30 no 97/63 0.10 0.15 0.10 90 E16 33/67 0.19 0.15 0.10 (1) The suspend!B|[ agent ess Metbocel 15, rather than Metbocel 10. Polyeerlzatlon Temperature, *C 53.5 53.5 53.5 53.5 53.5 53.5 53.5 59.5 53.5 56 56 56 56 56 56 56 56 56 67 57 Agitator Speed, rpe 300 300 300 300 300 300 400 400 300 350 350 300 350 300 390 350 300 350 144 143 Operating Pressure, pslg 141 147 149 113 133 137 136 113 113 133 138 136 130 130 13B 136 139 136 135 135 Beactlon Tine, hr 13 14.5 17 13 13 13 13 13 6 8 8.3 8.6 7.8 8.5 8 6 10 13 13.5 13 Terslnation Point Tine Pressure drop Pressure drop Tine 71m Tine Tlee T1m Tine Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop Pressure drop f B: 20:220-82 Autoclave: Agitation: Constant operating conditions: - 38 TABU VII SUSPKKSIOM POtnmIzatiok of vimvl chloride Snedltions lor Experimentation with Process 6 in Development Autoclave 8 see steel with clrculating-eater Jacket Mixco impellers and 4 aide-mounted baffles level, BO per cent; nonoeer-to-vater ratio, 33/87; concentration of dllauroyl peroxide catalyst, 0.08 per Sxpt to. 718 71B 720 731 783 Polyvlol V3 300 0.33 0.33 0.33 0,35 0.33 Barsolat 0.0875 0.0875 0.0075 0.07 0.0075 Calcine' Chloride 0.0473 0.0473 0.0473 0.045 0.0473 ` cent of TCI Calcium Carbonate Trichloro ethylene 0.0085 0.0005 0.0005 0.000 0.0005 1.5 1.5 1.5 1.0 - (1) Laurie acid la these polymerlxatin acollse ABL 70 free B. I. Laurie Acid (1) - 0.3 0.3 - Polfmerisatlon Temperature, *C 57 57 58 58 57 Agitator Speed, rps 350 350 350 350 350 Operating Pressure, palp 135 138 138 130 136 Sanction Time, hr 17.5 17 18 16 IS Termination Point 60 psig W PSig 46 psig 60 psig 00 psig 11:20:230-82 - 29 TABU VIII SUSPENSION POLYMER IZATION OP VIHYL CBLORIOE InlWtMf Pat for Process 5 and Process 6 Resin* Produced in Pilot-Scale Autoclaves (See Tables VI and VII for Operating Conditions) Expt Ro. Process 696 SS7 699 700 701 703 703 704 705 706 707 706 709 710 711 715 710 717 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Process 5 Bochs 5 Process 5 Process 5 716 719 730 731 733 Process 6 Process 6 Process 6 Process 6 6Process V 316-39 Process 5 316-30 Process 5 Specific Viscosity Apparent Density, lb/cu ft 0.164 0.167 0.165 0.190 0.180 0.166 0.182 0.109 0.181 0.165 0.171 0.167 0.170 0.175 0.171 0.173 0.167 0.167 17 31 25 34 17 14 12 19 8 30 27 27 27 38 26 27 36 21 0.131 0.131 0.133 0.136 0,176 38 33 33 31 36 0.174 4------------------------- 38 m ' *64* 66 197 337 49 70 64 60 60 54 83 70 103 48 36 41 39 60 53 Persorptlon, par cent _ - - -- - - - aio 1M 171 -- - isa Median. Microns Particle Characteristics__________ Dirougb 270-Menb, Dispersion Skev per cent >440 _ >440 >440 _ _ 110 - >440 _ 410 - 315 _ . >440 _ - _ - - _ 60 - 70 - 22 >440 . >440 * >440 - >440 - >440 a. - >440 - >440 _ - >440 -" 170 SIS 375 340 160 76 107 160 . 69 +0.03 +0.006 -0.46 0 s 16 10 16 2 155 66 +0.037 -lot OfAlllltOdv 6 Hard Resin Particles Per Square Foot on Mil Thickness 6------------ID--------------1775 _ ___ -- - _ __ -_ - _ -_ -- - -- - . _ . . _ _ . _ - - 10 30 75 200 10 70 10 20 30 30 10 200 40 30 30 -- - I CUT Hill Test Press Test 99 139 110 85 61. 91 118 93 136 103. Ill 121. 115 106 98. _ _ _ _ _ _ - 78 79 112. 120. 29+ 596161- * ----------------> O O' o oO cr> i J B:20:220-S2 - 30 - TABLE IX SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Status of Development of Process 5 and Process 6 Resins QXSM QYSM QXSM-5 QXSM-6 Target (Average) (C16-18W) (C16-10W) Specific viscosity Apparent density, lb/cu ft Absorption, per cent Median particle size, microns ICMT mill test Press "C" test Hard resin particles, per square foot on 17.5-mil film 0.170 32 50 150 >100 - 0.170 30 31 100 45 - <10 10 0.177 28 49 115 107+ 79+ 5 0.172 26 50 65 40+ 63 _ 30 NOTE: (1) The average values for QYSM resin are derived from Blend 134 through Blend 148. Some of the prop rtl s were not measured for all the blends, but the av rag Includes all available Information. (2) The examples used for QXSM-5 and QXSM-6 resin ar taken from specific runs which are considered representative of the over-all series. ucc 041047 B:20:220-S2 - 31 - TABLE X SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Status of Development of Process 5 and Process 6 Resins QXSJ Target QYSJ QXSJ-5 QXSJ-6 (Average) (C17-17W) (C17-12W) Specific viscosity Apparent density, lb/cu ft Absorption, per cent Median particle size, microns ICMT mill test Press "C" test Hard resin particles, per square foot on 17.5-mil film 0.145 32 50 150 >100 - 0.144 37 28 -- 59 - <10 9 0.143 30 47 145 106-173+ 0 0.139 31 35 55 97+ 73 ~ 5 NOTE: (1) The average values for QYSJ resin are deriv d from Blend 224 through Blend 230. Some of the properties were not measured for all the blends, but the av rag includes all available information. (2) The examples used for QXSJ-5 and QXSJ-6 resin are taken from specific runs which are considered representative of the over-all series. ucc 041048 ~1 B:20:220-32 - 32 - TABLE XI SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Status of Development of Process 5 Resins QXSA QYSA Target (Blend 2905) QXSA-5 (C16-21W) Specific viscosity Apparent density, lb/cu ft Absorption, per cent Median particle size, microns ICMT mill test Press "C" test Hard resin particles, per square foot on 17.5-mll film 0.115 32 - <200 - - <20 0.116 38 36 - 79 5 0.123 32 44 165 108 73 5 NOTE: The example of current production of QYSA repres nts a single blend, the only one for which data are now avail able. ucc 041049 4 B:20:220-82 - 33 - TABLE XII SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Status of Development of Process 5 Resins QXSC Specific viscosity Apparent density, lb/cu ft Absorption, per cent Median particle size, mdcrons ICMT mill test Press "C" test Hard resin particles, per square foot on 17.5-mil film Target 0.210 32 50 <200 >100 - <10 QXSC-5 (C15-22V) 0.217 30 51 US' 101+ 84 2 NOTE: Since QYSC resin has not been produced locally, regular production results cannot be presented. X: ucc 041050 I B:20:220-S2 APPENDIX A SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Comparison of the Calcium Carbonate and Calcium Chloride Used in Local Process 6 Polymerizations with the Materials Used in Germany Impurity Mg Si Fe A1 Cu CaC03 "local";------------ German, per cent per cent 0.01 0.01 0.2 o.os 0.1 0.1 0.001 ~EocaTT per cent 0.01 0.01 German) per cent 0.001 0.01 Total 0.02 0.451 0.02 o.on NOTE: These data mere obtained by semlquantitative analysis by the flame spectrometer and are considered reproducible within 30 per cent. ucc 041051 41 t B:20:220-32 APPENDIX B SUSPENSION POLYMERIZATION OF VINYL CHLORIDE Sampling and Testing Schedule during Production-Seal Experimentation with Process 5 and Process 6 Sample Autoclave Ingredients A. Ion-exchanged water used for the charge B. Suspending agent solution C. Autoclave water charge before catalyst addition Polymerization Slurries A. Hourly samples B. Final slurry after stripping (filtrate) C. Final slurry after stripping (resin) 1. Decants# wet resin 2. Tray-dried resin Flash-Dried Resin * ` "Iv' Tests pH, chloride ion, iron, surface tension, conductivity pH, total solids, gel analysis pH, chloride iron, iron, surface tension, conductivity pH, microscopic inspection ~ pH, chloride ion, iron, surface tension, conductivity wet-milling evaluation (optional), specific viscosity, heating loss,ICMT mill test specific viscosity, h ating loss, apparent density, siev analysis, absorption, hard resin particles at 6, 10, and 17.5 mils,ICMT mill test, 7905 preblend evaluation, photomicrographs at 75X ucc 041052 B:20:220-S2 DISTRIBUTION Mr. W. Adamson, NYO Mr. A. R. Anderson, 515 Mr. G. E. Brant, 514 Mr. J. W. Chatfield, 514 Mr. L. L. Dintiman, NYO Mr. J. C. Dotson, 514 Mr. D. H. Frodey, 514 Mr. R. D. Glenn, NYO Mr. G. J. Hanks, Jr., 514 Mr. J. L. Johnson, 514 Dr. J. L. Marsh, NYO Mr. J. C. McIntosh, 514 Mr. D. E. Richardson, 515 Mr. S. H. Rose (2), 511 Mr. M. E. Sutherland, 514 Mr. G. B. Telford, 514 Mr. R. N. Wheeler, 514 Mr. W. R. Wheeler, NYO Mr. J. W. Biddle Dr. J. J. Brezinskl Mr. D. L. Engle Mr. G. L. Funk Dr. R. I. Hoaglin Mr. R. G. Massey Mr. P. T. McCoy Dr. T. R. Miller Mr. A. E. Montagna Mr. C. R. Welter Library (2) INDEX LIST Calcium carbonate Calcium chloride Mersolat Methocel Polyviol VZ 200 Sodium bicarbonate Vinyl chloride Poly(vinyl chloride) Dilauroyl peroxide Fisheyes Heat stability Mixco agitation Pfaudler agitation 7 Particle size Resin physical properties Suspension polymeric zation Wacker processes 1 1 1 1 1 1 1 2 3 X X X X X X "X X ucc 041053